CN101602955A - The production technique of waste organic matter regeneration gasoline and diesel oil - Google Patents
The production technique of waste organic matter regeneration gasoline and diesel oil Download PDFInfo
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- CN101602955A CN101602955A CNA2008100117486A CN200810011748A CN101602955A CN 101602955 A CN101602955 A CN 101602955A CN A2008100117486 A CNA2008100117486 A CN A2008100117486A CN 200810011748 A CN200810011748 A CN 200810011748A CN 101602955 A CN101602955 A CN 101602955A
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Abstract
The production technique of waste organic matter regeneration gasoline and diesel oil is to belong to oiling worker field, particularly relates to the technology of plastic waste, tire, rubber item, chemical fibre, mineral wet goods production gasoline, diesel oil.The present invention just provides the production technique of a kind of efficient, energy-conservation, high safety, transparent waste organic matter regeneration gasoline and diesel oil.The present invention adopts following technical process, and its concrete steps are as follows: organism is pulverized mucus shape, hot cracked, dedusting sedimentation again, catalytic reforming, gas boil again after the hot melt extruded machine produces, flavor is dispelled in rectifying, separation, high frequency mr, sulfonation reaction, decolouring, gasoline and diesel oil are produced in petroleum products blending, ultra-sonic oscillation, leaching; Wherein catalytic reforming, dedusting sedimentation, three operations of thermo-cracking are vertically to contact successively; Rectifying, isolating noncondensable gas input gas electricity generator; The dispel thermal source of flavor, petroleum products blending of sulfonation reaction, decolouring is supplied with by light source of solar energy.
Description
Technical field:
The present invention belongs to oiling worker field, particularly relates to the technology of plastic waste, tire, rubber item, chemical fibre, mineral wet goods production gasoline, diesel oil.
Background technology:
Existing oiling technology is a lot, have nothing in common with each other, wherein more advanced as CN1099766A, the catalyzer that plastic waste elder generation depolymerization gas enters on cracking still and the porous sieve is again entering 200-250 ℃ of separation column fractionation, automatically controlled tower temperature at 300-380 ℃ of reaction cut gas, tower 1/2 place establishes two spouts, and the gas hydrocarbon coagulates for-10 through cooling
#Diesel oil, tower suitable position are established two mouths and are condensed into 70-90
#Gasoline; Residual oil returns the depolymerization again of depolymerization still at the bottom of the tower, oil product after filtration, with the gac carclazyte resultant corrected oil that decolours.
And for example disclosed plastic waste elder generation's pyrolysis of CN1084546A and then row cracking, the thermo-cracking hydrocarbon gas enter 300 ℃ of tower filling porcelains of 190 ℃ of tower bottoms of rectifying tower cat head ring gas and pass through to cat head from the slit, and side line is a heavy oil at the bottom of fractionating out gasoline, diesel oil, tower.Establish evaporator tower on the cracking still, tower filling porcelain ring gas rushes at separation column from the slit.
The plastics depolymerization was poured the separation column straight-forward fractional distillation at cracking cut gas during CN1099766A openly reported, and use equipment is less.The tower valve but above-mentioned two patents easily bond, even stop up the tower valve; With gac or clay treatment, its oil product colloid exist part unconverted, oil colours is dark deeply.
Add catalyzer again after the pyrolysis of plastic waste elder generation during CN1084546A openly reports and carry out cracking, the hydrocarbon gas enters rectifying tower, and inner-tower filling material is the porcelain ring, is gasoline after the overhead gas condensation, and tower middle part gas hydrocarbon is condensed into diesel oil, and tower bottom is a heavy gas oil.Noncondensable gas is made fuel behind the water seal spark arrester.
This method is similar to the first two method, and difference is a filling porcelain ring, and the easiest assembly glue pledge of porcelain czermak space when temperature is low, was then stubbornly refused gas admittedly, and the two all with the naked light heating, exists disaster hidden-trouble, shortcomings such as oil quality difference.
Summary of the invention:
The present invention is exactly at the problems referred to above, and the production technique of a kind of efficient, energy-conservation, high safety, transparent waste organic matter regeneration gasoline and diesel oil is provided.
For achieving the above object, the present invention adopts following technical process, and its concrete steps are as follows:
Organism pulverized mucus shape, hot cracked, dedusting sedimentation again, catalytic reforming, gas boil again after the hot melt extruded machine produces, flavor is dispelled in rectifying, separation, high frequency mr, sulfonation reaction, decolouring, gasoline and diesel oil are produced in petroleum products blending, ultra-sonic oscillation, leaching;
Wherein catalytic reforming, dedusting sedimentation, three operations of thermo-cracking are vertically to contact successively;
Rectifying, isolating noncondensable gas input gas electricity generator;
The dispel thermal source of flavor, petroleum products blending of sulfonation reaction, decolouring is supplied with by light source of solar energy.
Beneficial effect of the present invention:
1, high-level efficiency:
The gasoline of explained hereafter of the present invention, diesel oil high-level efficiency, such as, the 500Kg plastic waste produces 90
#Gasoline 140Kg ,-10
#10.6 kilowatts of diesel oil 186Kg, coarse carbon black 146Kg, generatings, whole technological process is only used 6 hours at the most;
2, security is good:
In the production technique of the present invention without exception without naked light, but electrically heated, so security is good;
3, energy-conservation:
Three operations of the catalytic reforming in the technology of the present invention, dedusting sedimentation, thermo-cracking are vertically to contact successively, and the material of complete reaction can not got back to thermo-cracking once more, and to the greatest extent it is used to make raw material; In addition, utilize the noncondensable gas generating of this technology; Sulfonation reaction, the flavor of dispelling that decolours, the thermal source of petroleum products blending is supplied with by sun power.
Description of drawings:
Fig. 1 is a process flow sheet of the present invention.
Embodiment:
Organism pulverized mucus shape, hot cracked, dedusting sedimentation again, catalytic reforming, gas boil again after the hot melt extruded machine produces, flavor is dispelled in rectifying, separation, high frequency mr, sulfonation reaction, decolouring, gasoline and diesel oil are produced in petroleum products blending, ultra-sonic oscillation, leaching;
Wherein catalytic reforming, dedusting sedimentation, three operations of thermo-cracking are vertically to contact successively;
Rectifying, isolating noncondensable gas input gas electricity generator;
The dispel thermal source of flavor, petroleum products blending of sulfonation reaction, decolouring is supplied with by light source of solar energy.
Embodiment:
Get plastic waste 500Kg and pulverize, add 170 ℃ of hot melt material-extruding machine 1 controlled temperature successively, plastic waste is molten into the mucus shape and gets into cracking still 2, and temperature in the kettle is not less than 230 ℃;
320～400 ℃ of tensimeter demonstration-0.01mPa of cracking still 2 controlled temperature; Carry out scission reaction, produce the gas hydrocarbon through settling vessel 3, cracking still 2 does not fall back in gasification substance, continues cracking, and the gas hydrocarbon then enters catalytic reforming jar 4;
The gas hydrocarbon enters the catalyzer (number of patent application: 200610047167.9) carry out the catalyzed reaction macromolecular chain and be fractured into small molecules or monomer on catalytic reforming jar 4 and the fixed bed; The catalyzed reaction temperature is controlled in 280 ℃～360 ℃, the gas air inlet body reboiler 5 after the catalyzed reaction.
Gas enters gas reboiler 5 and continues thermal degradation, and temperature is controlled at 400～420 ℃ and impels the heavy component lighting to enter separation column 8 fractionation again.(tower top controlled temperature is not less than 130 ℃);
Mix the hydrocarbon gas and enter separation column 8 and carry out the mass-and heat-transfer reaction, eight layers of column plates installing bubble-cap cut down, and gas is cut diesel oil through fluid-tight section generation mass-and heat-transfer reaction side line, reach the standard grade and cut gasoline, and heavy hydrocarbons falls that fluid reservoir returns cracking still 2 under tower; Condensing does not separate from cat head.
Separation column 8 cuts diesel oil and enters and separate diesel fuel tank 11, cuts gasoline and enters and separate after the gasoline tank 10 that moisture content is discharged in water collector awl end under the tank body, oil is transported to high frequency magnetic field producer 12.
Oil product enters high frequency magnetic field producer 12 and adopts 6～8 Gigahertz/seconds of operating frequencies.To macromolecular chain in the oil product carry out large amplitude how tangentially to cut apart intermolecularly put in order, the disconnected small molecule monomer that is cut into.The raising oil recovery rate is analysed and is separated colloid, and temperature keeps about 60 ℃.
Oil pump 13 behind the TURP is gone into sulfonation jar 14 and is spilled into 99% vitriol oil by 3～5% of weight of oil, 0.1～0.5% Tai-Ace S 150, stirring 15min are heated to 45～55 ℃, blow with pressurized air and bore sharp valve discharge black colloid condensation product down from jar after 3min leaves standstill 3～4h.Give a baby a bath on the third day after its birth time with 50 ℃ of water purification and to stir three times (leaving standstill 1h) and discharge three times, pump into bleacher 15 then.(add coiled pipe and solar heater 21 in the thermal recovery jar, communication loop, jar is provided with the thermostatically controlled valve steady temperature).
Oil product after the sulfonation reaction pumps into bleacher 15, adding concentration by 10～20% of weight of oil is 30% sodium hydroxide (potassium) solution stirring 15min, 40～50 ℃ of coil pipe heating, temperature leaves standstill 3～4h in constant jar, behind jar lower valve gate discharge cash slag liquid, wash once, add 1～4% thiosulphate after discharging water again with 50 ℃ of water purification.Stir 10min, leave standstill 1～2h, the discharge raffinate adds 50 ℃ of 5～7% active white sands, the heating of 2～3% root of Dahurain angelica particles then with hot water wash secondary (by the washing operation), and stirring, air-blowing 10 minutes are left standstill 3～4h and divided a jar solids, and oil product is clear thorough faint yellow.Pump into the flavor jar of dispelling.
Oil product pumps into the flavor jar 16 of dispelling, and (root of Dahurain angelica, Radix Glycyrrhizae, the Tai-Ace S 150 patent application patent No.: 200610047169.9) 8-10% oil temperature is constant leaves standstill 4h at 55 ℃ of stirring 10min, and the oil product free from extraneous odour is respectively put fragrant to add the flavor agent of dispelling by weight of oil.Separation decorating film, fluid pump into the blending retort.
Fluid pumps into tempering tank 17, should check its index to add different amount ratios in different indexes then respectively to vapour, diesel oil; T501, sanitas, octane value conditioning agent, cetane value growth promoter, ignition dope, purification agent etc. stir, check up to standard till.Qualified oil product flows into ultrasonic oscillator 18.
Oil product enters ultrasonic oscillator 18, fluid and produces the molecular chain interaction force in oscillation frequency under the large-amplitude vibration of 6.2～6.5 ten thousand hertz/sec and make approaching, the therefore static stability in storage height of avidity, and whole process is no more than 10min, constant 52 ℃ of oil temperature.
Fluid pumps into leaching tower 19 behind sonic oscillation, fluid is gone into shower nozzle in the tower from cat head and is spilt and drench on column plate, four layers of column plate load active white sand, root of Dahurain angelica grain, filter screen 800～2000 orders, filter felt 800 orders, filter cloth 400 orders, filter paper respectively, and fluid slowly soaks to drench and splashes under the tower accumulator and staticly settle the back and flow into processed oil storage tank 20 and can dispatch from the factory.
Cracking still 2 produces coarse carbon blacks and decontrols cracking still 2 bottom residual cake valves when making sludge-store cabin 6 show negative pressure 6kma down in that the suction of vacuum pump 7 is moving, but start the agitator carbon black suck sludge-store cabin 6 through the recirculated water cooling, stir exothermic temperature and when 300 ℃ are reduced to 70 ℃, emit through rotary conveyor 22, defeatedly store up slag bath 23 entruckings and sell.
Hydrogen sulfide in the combustible gas that discharge on separation column 8 top enter digester 24, with jar in an iron oxide solution contact reacts be iron sulphide, after transfer ferric oxide again to, hydrogen then closes with water-soluble.Combustion gas after the purification enters the assorted neutralization tank 25 of dispelling, gas and jar interior cash liquid reaction decomposes ester class, soap class polygamy thing.And gas enters drying tower 26 at siccative after carrying out thorough washing, enter strainer 27 after the absorption of gac, gas purifies from filter core after gas compressor 28, sends electric energy and enter store battery 30, outward current by invertor power supply machine, electric heating, illumination but enter fuel gas generation unit 29.
Claims (8)
1, the production technique of waste organic matter regeneration gasoline and diesel oil, it is characterized in that adopting following technical process, its concrete steps are as follows: organism is pulverized mucus shape, hot cracked, dedusting sedimentation again, catalytic reforming, gas boil again after the hot melt extruded machine produces, flavor is dispelled in rectifying, separation, high frequency mr, sulfonation reaction, decolouring, gasoline and diesel oil are produced in petroleum products blending, ultra-sonic oscillation, leaching;
Wherein catalytic reforming, dedusting sedimentation, three operations of thermo-cracking are vertically to contact successively;
Rectifying, isolating noncondensable gas input gas electricity generator;
The dispel thermal source of flavor, petroleum products blending of sulfonation reaction, decolouring is supplied with by light source of solar energy.
2, the production technique of waste organic matter regeneration gasoline and diesel oil according to claim 1, it is characterized in that getting plastic waste and pulverize, add successively 170 ℃ of hot melt material-extruding machine (1) controlled temperature, plastic waste is molten into the mucus shape and gets into cracking still (2), and temperature in the kettle is not less than 230 ℃.
3, the production technique of waste organic matter regeneration gasoline and diesel oil according to claim 1 is characterized in that 320～400 ℃ of tensimeter demonstration-0.01mPa of cracking still (2) controlled temperature; Carry out scission reaction, produce the gas hydrocarbon through settling vessel (3), cracking still (2) does not fall back in gasification substance, continues cracking, and the gas hydrocarbon then enters catalytic reforming jar (4).
4, the production technique of waste organic matter regeneration gasoline and diesel oil according to claim 1 is characterized in that the gas hydrocarbon enters the catalyzer on catalytic reforming jar (4) and the fixed bed, carries out the catalyzed reaction macromolecular chain and is fractured into small molecules or monomer; The catalyzed reaction temperature is controlled in 280 ℃～360 ℃, the gas air inlet body reboiler (5) after the catalyzed reaction.
5, the production technique of waste organic matter regeneration gasoline and diesel oil according to claim 1 is characterized in that gas enters gas reboiler (5) and continues thermal degradation, and temperature is controlled at 400～420 ℃ and impels the heavy component lighting to enter separation column (8) fractionation again; Mix the hydrocarbon gas and enter separation column (8) and carry out the mass-and heat-transfer reaction, eight layers of column plates installing bubble-cap cut down, and gas is cut diesel oil through fluid-tight section generation mass-and heat-transfer reaction side line, reach the standard grade and cut gasoline, and heavy hydrocarbons falls that fluid reservoir returns cracking still (2) under tower; Condensing does not separate from cat head.
6, the production technique of waste organic matter regeneration gasoline and diesel oil according to claim 1 is characterized in that oil product enters high frequency magnetic field producer (12) and adopts 6～8 Gigahertz/seconds of operating frequency.
7, the production technique of waste organic matter regeneration gasoline and diesel oil according to claim 1, it is characterized in that oil product enters ultrasonic oscillator (18), fluid at the large-amplitude vibration of oscillation frequency in 6.2～6.5 ten thousand hertz/sec, whole process is no more than 10min, constant 52 ℃ of oil temperature.
8, the production technique of waste organic matter regeneration gasoline and diesel oil according to claim 1 is characterized in that gas purifies after gas compressor (28) enters fuel gas generation unit (29) from filter core, send electric energy and enter store battery (30).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2008100117486A CN101602955B (en) | 2008-06-11 | 2008-06-11 | Production process of waste organic matter for regeneration of gasoline and diesel oil |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2008100117486A CN101602955B (en) | 2008-06-11 | 2008-06-11 | Production process of waste organic matter for regeneration of gasoline and diesel oil |
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| Publication Number | Publication Date |
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| CN101602955A true CN101602955A (en) | 2009-12-16 |
| CN101602955B CN101602955B (en) | 2013-07-17 |
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| CN2008100117486A Expired - Fee Related CN101602955B (en) | 2008-06-11 | 2008-06-11 | Production process of waste organic matter for regeneration of gasoline and diesel oil |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102408906A (en) * | 2011-10-25 | 2012-04-11 | 中国科学院广州能源研究所 | Method for preparing lubricating oil base oil from waste and old plastics |
| CN102504865A (en) * | 2011-11-15 | 2012-06-20 | 安徽盈荣生物能源科技有限公司 | Method for refining diesel oil or gasoline by using waste oil |
| CN102786980A (en) * | 2012-08-01 | 2012-11-21 | 山东汇科通用机械有限公司 | Waste plastic oil refining production method and production line thereof |
| CN103820148A (en) * | 2014-01-23 | 2014-05-28 | 周文彬 | Used mineral oil full-automatic control catalytic cracking environment-friendly integrated refining equipment and process |
| CN105778970A (en) * | 2015-06-01 | 2016-07-20 | 安徽科茂能源科技有限公司 | Safe and environment-friendly oil refining technology achieving cracking recycling of waste organic matter by means of continuous feeding and slag discharging |
| CN106190213A (en) * | 2015-04-30 | 2016-12-07 | 雷建光 | A kind of technique utilizing household refuse landfill sites waste or used plastics to extract gasoline, diesel |
| CN111040806A (en) * | 2018-10-11 | 2020-04-21 | 王雨田 | Full-sealed continuous pyrolysis kettle |
| CN114806644A (en) * | 2022-06-06 | 2022-07-29 | 北京清创晋华科技有限公司 | Pyrolysis gasifier |
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| CN2350395Y (en) * | 1998-10-26 | 1999-11-24 | 北京绿神环保技术有限公司 | Apparatus for continuous producing fuel oil using waste plastics |
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| CN101074385A (en) * | 2007-04-28 | 2007-11-21 | 牛斌 | Waste-plastic continuous cracking process and cracker |
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Patent Citations (5)
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| CN1080312A (en) * | 1992-06-20 | 1994-01-05 | 彭培安 | Method and device thereof with production of fuel from waste plastics |
| CN2350395Y (en) * | 1998-10-26 | 1999-11-24 | 北京绿神环保技术有限公司 | Apparatus for continuous producing fuel oil using waste plastics |
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Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102408906A (en) * | 2011-10-25 | 2012-04-11 | 中国科学院广州能源研究所 | Method for preparing lubricating oil base oil from waste and old plastics |
| CN102504865A (en) * | 2011-11-15 | 2012-06-20 | 安徽盈荣生物能源科技有限公司 | Method for refining diesel oil or gasoline by using waste oil |
| CN102786980A (en) * | 2012-08-01 | 2012-11-21 | 山东汇科通用机械有限公司 | Waste plastic oil refining production method and production line thereof |
| CN102786980B (en) * | 2012-08-01 | 2015-09-23 | 山东汇科通用机械有限公司 | A kind of waste plastic oil-refining production method and production line thereof |
| CN103820148A (en) * | 2014-01-23 | 2014-05-28 | 周文彬 | Used mineral oil full-automatic control catalytic cracking environment-friendly integrated refining equipment and process |
| CN106190213A (en) * | 2015-04-30 | 2016-12-07 | 雷建光 | A kind of technique utilizing household refuse landfill sites waste or used plastics to extract gasoline, diesel |
| CN105778970A (en) * | 2015-06-01 | 2016-07-20 | 安徽科茂能源科技有限公司 | Safe and environment-friendly oil refining technology achieving cracking recycling of waste organic matter by means of continuous feeding and slag discharging |
| CN105778970B (en) * | 2015-06-01 | 2017-07-11 | 安徽科茂能源科技有限公司 | A kind of continuous feed, the safety and environmental protection oil refining process of the waste and old organic cracking regeneration of deslagging |
| CN111040806A (en) * | 2018-10-11 | 2020-04-21 | 王雨田 | Full-sealed continuous pyrolysis kettle |
| CN114806644A (en) * | 2022-06-06 | 2022-07-29 | 北京清创晋华科技有限公司 | Pyrolysis gasifier |
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| CN101602955B (en) | 2013-07-17 |
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Address after: 124000, room 1, unit 2, Fu Hua Town, Shuangtaizi District, Liaoning, Panjin 1107, China Patentee after: Dou Hongbo Address before: 110003, No. 6-7, building -3, Tai second district, Tiexi District, Liaoning, Shenyang Patentee before: Dou Hongbo |
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